The present invention refers to the processing of a 100% renewable load in FCC units, wherein the load comprises triglycerides of vegetable and animal source, free fatty acids, fatty acid esters, ketones, alcohols and long-chain aldehydes, using catalyst and appropriate operating conditions in order to obtain 100% renewable products with a high content of aromatic compounds, in the range of naphtha, kerosene, diesel and heavy gas oil. The product thus obtained complies with all the properties of the ASTM D1655 standard, even for contents of up to 10% renewable content. In addition, there is no need to reduce the freezing point of the fossil QAV for the introduction of the renewable component, with no impact on the yield and economy of the process.

The present invention relates to a process for producing mixture of fuel components, which process comprises providing a feed of biological origin; subjecting said feed of biological origin and a hydrogen gas feed to a single step of hydroprocessing in the presence of a catalyst system comprising dewaxing catalyst to form a mixture of fuel components. The present invention relates also to an apparatus for producing a mixture of fuel components from a feed of biological origin. The invention relates also to the use of the fuel components.

A catalyst and corresponding methods of using a catalyst are provided that can be beneficial for conversion of paraffins into a product stream enriched in aromatics and/or methane while reducing or minimizing the content of ethane in the product stream. Such catalysts and methods can be useful, for example, for processing a raw gas, associated gas, tail gas, natural gas, or other type of methane-containing feed stream to convert C.sub.2+ hydrocarbons in the stream to heavier hydrocarbons and methane while reducing or minimizing content of ethane in the products from the conversion reaction. Such conversion can be useful for upgrading a methane-containing feed stream to have an energy content that is suitable for pipeline transport under one or more specifications for transport of natural gas. The catalyst and corresponding method can also be beneficial when used as a second stage catalyst in a configuration involving multiple conversion stages.

The present invention relates to the use of adsorbents comprising zinc oxide nanowires decorated with catalytically active metal particles for the removal of sulfur from hydrocarbon feedstocks, including the desulfurization of diesel fuels and the deep desulfurization of natural gas, and to the use of decorated zinc oxide nanowire adsorbents for the hydrogenation of naphthalene selectively to tetralin in the presence of sulfur compounds. The adsorbent comprises nickel metal particles or nickel-zinc alloy particles deposited on zinc oxide nanowires.

A non-petroleum or renewable feedstock containing oxygen and contaminants of metals, gums, and resins is treated by introducing the feedstock into a reactor at a flow velocity of from 20 ft/sec to 100 ft/sec. The feedstock is heated within the reactor to a temperature of from 700° F. to 1100° F. to remove and/or reduce the content of the contaminants to form a reactor product. The reactor product is cooled to form a cooled reactor product. Non-condensable gases, metals and water are separated and removed from the cooled reactor product to form a final product. The final product has an oxygen content that is 60% or less of that of the feedstock, and wherein the final product comprises 25 wt % or less any triglycerides, monoglycerides, diglycerides, free fatty acids, phosphatides, sterols, tocopherols, tocotrienols, or fatty alcohols, from 5 wt % to 30 wt % naphtha, and 50 wt % or more diesel.

The invention relates to a continuous process for converting carbonaceous material contained in one or more feedstocks into a liquid hydrocarbon product, said feedstocks including the carbonaceous material being in a feed mixture including one or more fluids, said fluids including water and further liquid organic compounds at least partly produced by the process in a concentration of at least 1% by weight, where the process comprises converting at least part of the carbonaceous material by pressurizing the feed mixture to a pressure in the range 250-400 bar; heating the feed mixture to a temperature in the range 370-450° C., and maintaining said pressurized and heated feed mixture in the desired pressure and temperature ranges in a reaction zone for a predefined time; cooling the feed mixture to a temperature in the range 25-200° C. and expanding the feed mixture to a pressure in the range of 1-70 bar, thereby causing the carbonaceous material to be converted to a liquid hydrocarbon product and separating from the converted feed mixture a fraction comprising liquid hydrocarbon product.

The present disclosure is related to a multistep process for producing renewable gasoline components from a glyceride containing feedstock. The glycerides are split to provide a stream containing fatty acids, or esters of fatty acids, and another stream containing glycerol and water. Glycerol, preferably as crude glycerol recovered from splitting, is next converted to propanols at vapor phase, providing a renewable propanol gasoline component. Another renewable gasoline component is obtained from hydroprocessing of the fatty acids or esters thereof, as a renewable paraffinic naphtha component. Blending the renewable components can provide a novel 100% renewable gasoline.

The invention relates to a catalytic process for upgrading a renewable crude oil produced from biomass and/or waste comprising providing a renewable crude oil and pressurizing it to a pressure in the range in the range 60 to 150 bar, contacting the pressurized renewable crude oil with hydrogen and at least one heterogeneous catalyst contained in a first reaction zone at a weight based hourly space velocity (WHSV) in the range 0.1 to 2.0 h.sub.−1 and at a temperature in the range of 150° C. to 360° C., hereby providing a partially upgraded renewable crude oil, separating the partially upgraded renewable crude oil from the first reaction zone to a partially upgraded heavy renewable oil fraction, a partially upgraded light renewable oil fraction, a water stream and a process gas stream, introducing the separated and partially upgraded heavy renewable oil fraction and separated process gas to a second reaction zone comprising at least two reactors arranged in parallel and being adapted to operate in a first and a second mode of operation, the reactors comprising dual functioning heterogeneous catalyst(-s) capable of performing a catalytic steam cracking reaction in a first mode of operation or a steam reforming reaction in a second mode of operation, where the partially upgraded heavy renewable oil fraction from the first reaction zone is contacted with the dual functioning heterogeneous catalyst and steam at a pressure of 10 to 150 bar and a temperature of 350° C. to 430° C. whereby a catalytic steam cracking of the partially upgraded heavy renewable oil is performed in the reactors in the first mode of operation, hereby providing a further upgraded heavy renewable oil fraction, while separated process gas from the first and/or second reaction zone is contacted with the dual functioning catalyst and steam at a pressure of 0.1 to 10 bar and a temperature of 350 to 600° C. in the reactors in the second mode of operation and contacted with the dual functioning catalyst, thereby producing a hydrogen enriched gas, separating the further upgraded heavy renewable oil fraction from the catalytically steam cracking reactor to at least one light renewable oil fraction, a heavy renewable oil fraction, a hydrogen rich process gas and a water phase, separating hydrogen from the hydrogen enriched gas from the catalytic steam cracking zone and/or from the catalytic steam reforming and recycling it to the first reaction zone, alternating the reactors between the first mode of operation and the second mode of operation at predetermined time intervals thereby allowing for regeneration of the heterogeneous catalyst for the catalytic steam cracking in the first mode of op

Processes for the treatment of waste streams from the hydroconversion of heavy hydrocarbons containing additives and catalysts are described. At least one of the SHC pitch stream, SDA pitch stream, and the heavy residue stream is sent to a thermal oxidation system. The metals in the SHC and SDA pitch streams and the heavy residue stream are oxidized and can be easily recovered as clean powdered metal oxides which can be reused or sold. The processes produce chemicals which can be recovered and sold.

In the hydroconversion processes of heavy hydrocarbon oils, in which the hydrogen is introduced at the reactor base by bubbling, the low diffusion rate of hydrogen, from the gas phase to the reaction liquid, limits the degree of conversion. The process circumvents the obstacle of the limited amount of reactant hydrogen by using a slurry bubble column reactor which reduces the formation of light hydrocarbon products, and therefore the hydrogen required for the hydroconversion, allowing to operate at full conversion.